WO2003080512A1 - Method and device for producing a metal hydroxide - Google Patents
Method and device for producing a metal hydroxide Download PDFInfo
- Publication number
- WO2003080512A1 WO2003080512A1 PCT/EP2003/002859 EP0302859W WO03080512A1 WO 2003080512 A1 WO2003080512 A1 WO 2003080512A1 EP 0302859 W EP0302859 W EP 0302859W WO 03080512 A1 WO03080512 A1 WO 03080512A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- filter
- suspension
- permeate
- filtered
- metal
- Prior art date
Links
- 238000000034 method Methods 0.000 title claims abstract description 48
- 229910000000 metal hydroxide Inorganic materials 0.000 title claims abstract description 24
- 150000004692 metal hydroxides Chemical class 0.000 title claims abstract description 24
- 239000012466 permeate Substances 0.000 claims abstract description 39
- 239000000725 suspension Substances 0.000 claims abstract description 36
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 claims abstract description 22
- 239000000347 magnesium hydroxide Substances 0.000 claims abstract description 22
- 229910001862 magnesium hydroxide Inorganic materials 0.000 claims abstract description 22
- 239000012266 salt solution Substances 0.000 claims abstract description 22
- 238000009295 crossflow filtration Methods 0.000 claims abstract description 21
- 229910052751 metal Inorganic materials 0.000 claims abstract description 16
- 239000002184 metal Substances 0.000 claims abstract description 16
- 238000001914 filtration Methods 0.000 claims abstract description 11
- 239000012141 concentrate Substances 0.000 claims description 23
- 238000001223 reverse osmosis Methods 0.000 claims description 21
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 18
- 150000003839 salts Chemical class 0.000 claims description 16
- 238000006243 chemical reaction Methods 0.000 claims description 14
- 239000012528 membrane Substances 0.000 claims description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 11
- 239000000243 solution Substances 0.000 claims description 9
- 239000011148 porous material Substances 0.000 claims description 8
- 238000001556 precipitation Methods 0.000 claims description 7
- 238000004519 manufacturing process Methods 0.000 claims description 5
- 238000004140 cleaning Methods 0.000 claims description 4
- 230000001376 precipitating effect Effects 0.000 claims description 4
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 3
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 3
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 3
- 238000000605 extraction Methods 0.000 claims description 3
- 239000004571 lime Substances 0.000 claims description 3
- 239000008267 milk Substances 0.000 claims description 3
- 210000004080 milk Anatomy 0.000 claims description 3
- 235000013336 milk Nutrition 0.000 claims description 3
- 239000011780 sodium chloride Substances 0.000 claims description 3
- 238000009434 installation Methods 0.000 abstract 2
- 238000011045 prefiltration Methods 0.000 description 7
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 6
- 229910052749 magnesium Inorganic materials 0.000 description 6
- 239000011777 magnesium Substances 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 230000000717 retained effect Effects 0.000 description 4
- 238000011144 upstream manufacturing Methods 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- 239000000654 additive Substances 0.000 description 2
- 230000000996 additive effect Effects 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000013535 sea water Substances 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical class [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 1
- 239000004480 active ingredient Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 235000011116 calcium hydroxide Nutrition 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 239000003599 detergent Substances 0.000 description 1
- 238000007865 diluting Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 239000013505 freshwater Substances 0.000 description 1
- 150000004679 hydroxides Chemical class 0.000 description 1
- 238000001471 micro-filtration Methods 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 210000002784 stomach Anatomy 0.000 description 1
- 239000012498 ultrapure water Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/025—Reverse osmosis; Hyperfiltration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/04—Feed pretreatment
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/14—Ultrafiltration; Microfiltration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/14—Ultrafiltration; Microfiltration
- B01D61/147—Microfiltration
- B01D61/1471—Microfiltration comprising multiple microfiltration steps
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/58—Multistep processes
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
- C01B13/14—Methods for preparing oxides or hydroxides in general
- C01B13/36—Methods for preparing oxides or hydroxides in general by precipitation reactions in aqueous solutions
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F5/00—Compounds of magnesium
- C01F5/14—Magnesium hydroxide
- C01F5/22—Magnesium hydroxide from magnesium compounds with alkali hydroxides or alkaline- earth oxides or hydroxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/04—Specific process operations in the feed stream; Feed pretreatment
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/14—Ultrafiltration; Microfiltration
- B01D61/145—Ultrafiltration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/14—Ultrafiltration; Microfiltration
- B01D61/147—Microfiltration
Definitions
- the invention relates to a method and a device for producing a metal hydroxide, in particular magnesium hydroxide, according to the preambles of claims 1 and 20, respectively.
- Metal hydroxides are raw materials that are needed industrially in many different ways. This applies in particular to magnesium hydroxide, which is used, for example, to purify flue gases and in wastewater treatment. Pure magnesium hydroxide is used in particular as an additive for detergents, as an additive in plastics processing and as a pharmaceutically active ingredient in stomach preparations.
- Metal hydroxides come in many different forms in nature.
- magnesium hydroxide occurs as bruzite. To date, it is mainly obtained from final lye from potash salt processing or by precipitation from sea water, which contains an average of approx. 0.5% magnesium. Lime milk is usually added to both liquids, i.e. the final lye or sea water, as a result of which magnesium hydroxide is precipitated from the liquids. Then it is separated in filter presses. Similar processes are known for other metal hydroxides.
- the known methods have the disadvantage that the deposition of the magnesium hydroxide requires large filter areas and long filter times because of a greasy precipitation in the liquids mentioned. This leads to long and expensive manufacturing processes and to expensive and complex structural measures in the manufacturing device.
- the invention is therefore based on the object of specifying a method and a device for producing a metal hydroxide, by means of which simple, inexpensive and rapid production of the metal hydroxide in high purity is made possible.
- This object is characterized according to the invention with a method for producing a metal hydroxide with the features of claim 1.
- a device for performing in particular the method according to the invention is characterized by the features of claim 20.
- the metal is first precipitated from a salt solution in the form of hydroxide. This creates a suspension. This suspension is then filtered. A cross-flow filter technology is now used for this: the saline-containing suspension is filtered through a filter using the cross-flow filter technology. A permeate formed during the filtering of the salt solution-containing suspension is fed back to the cross-flow filtration system, which is preferably a return of the permeate to the cross-flow filtration system.
- the invention is based on the knowledge that the particles produced by the precipitation are predominantly transported in the flow core in the crossflow filtration because of the turbulent flow conditions present here. Due to the turbulent flow conditions, a uniform washout of dissolved foreign substances is made possible.
- the solution containing the metal hydroxide is cleaned repeatedly with the permeate, which becomes increasingly salt-free, so that disruptive foreign substances can be separated from this solution in any concentration.
- the suspension containing the metal hydroxide is continuously freed of salts and other substances. It is thus possible to obtain metal hydroxide in a very good quality in a simple manner.
- the permeate of a filter is fed to at least one other filter of the crossflow filtration system.
- This is preferably understood to mean the return of the permeate from one filter to the other filter.
- the salt solution-containing suspension is filtered by means of a membrane filter.
- the membrane filter preferably has pores which have a pore size of up to 30 micrometers. In a particularly preferred embodiment, the pore size is between 0.05 and 0.5 micrometers.
- the salt solution for precipitating the metal is preferably fed to a reaction vessel in which the metal is precipitated in the form of hydroxide. Furthermore, it is preferably provided after the filtering to clean a concentrate obtained from the filter for the final extraction of the metal hydroxide.
- the salt solution which contains the metal is made alkaline in a reaction container.
- the metal is precipitated in the form of a hydroxide, which is very finely dispersed in a suspension which was produced by the precipitation.
- the suspension is preferably fed to a working container which is connected to a cross-flow filtration system, for example an ultra or a microfiltration system.
- a permeate which is in the form of a metal hydroxide-free salt solution, is preferably separated off via a membrane filter.
- the permeate is passed to a reverse osmosis unit, provided the content of dissolved salts is not so high that the reverse osmosis unit cannot process it.
- the concentrate retained by the membrane filter contains a concentrated suspension with metal hydroxide, which is preferably returned to the working container.
- the working tank also receives pure water, which is used to rinse out other soluble salts.
- the pure water is preferably taken from the reverse osmosis unit.
- the concentrate formed during reverse osmosis, which contains the soluble salts in particular, is discharged. This means that it is no longer used for the method according to the invention.
- the embodiment described above has the advantage that the suspension containing the metal hydroxide is continuously freed of salts and other substances which are discharged as concentrates via the reverse osmosis unit.
- the above-mentioned embodiment is based on the following considerations: Due to the highly turbulent flow conditions inherent in cross-flow filtration systems, the filtration process acts as a mixing element, so that a very uniform washout of dissolved foreign substances is made possible. Due to the intensive mixing, a very small grain is produced in the suspension, since the turbulent flow control prevents the formation of agglomerates in the suspension and the agglomerates formed are broken up.
- the saline-containing suspension is filtered by means of at least two filters, a first filter being arranged or connected in front of a second filter.
- filters are preferably each arranged in a filter stage, which are connected in series.
- the permeate passing through the second filter is led back to the first filter.
- At least one filter or at least one of the filter stages is supplied with pure water for rinsing out at least one soluble salt from the suspension which formed during the precipitation of the metal from the salt solution.
- the permeate leaving the first filter stage or the first filter is fed to a reverse osmosis unit, provided that the salt concentrations - as already described above - allow this.
- the pure water obtained by means of the reverse osmosis unit is preferably fed to the second filter or the filter stage. It is further preferably provided that the permeate leaving the filter of the second filter stage is fed to the first filter stage.
- All of the above-mentioned exemplary embodiments are based on the principle of countercurrent extraction.
- Several crossflow filtration stages are connected in series or operated one after the other (ie used several times in succession), the last crossflow filtration stage preferably receiving a salt-free permeate from reverse osmosis.
- the final crossflow filtration stage then leaves a concentrate that has been washed with salt-free permeate.
- the permeate of this crossflow filtration stage which is now only slightly contaminated with dissolved salts, is then fed to the previous crossflow filtration stage for washing out the salts present there.
- this countercurrent process can be used to produce metal hydroxide in virtually any purity. Another advantage is that the amount of pure water required for cleaning is reduced.
- the metal is precipitated using milk of lime or sodium hydroxide solution.
- the device according to the invention for performing in particular the method described above is characterized by the features of claim 20. It has at least one reaction container or reaction unit for precipitating the metal from the salt solution and at least one filter stage, which has at least one filter, for filtering the salt solution-containing suspension resulting from the precipitation. A permeate penetrates through the filter. Furthermore, at least one line for feeding or returning the permeate into at least one of the filter stages is provided.
- Figure 1 is a schematic diagram of a first device for
- Figure 2 is a schematic diagram of a second device for performing the method, wherein magnesium hydroxide is generated from a concentrate
- Figure 3 is a schematic diagram of a third device for performing a further method, wherein magnesium hydroxide is generated from a concentrate.
- FIG. 1 shows a basic illustration of a first device according to the invention for carrying out the method according to the invention, in which magnesium hydroxide is produced from a concentrate.
- the individual structural units are explained in more detail on the basis of the description of the method according to the invention.
- a salt solution containing magnesium is fed to a reaction container 1 in which the solution is made alkaline by adding lime milk or sodium hydroxide solution. After a pH of approx. 11.5 has been reached, all of the magnesium has precipitated in the form of hydroxide and is finely dispersed in the suspension formed in this way.
- the suspension is then fed to a working container 2 which is connected to a filtration stage 3.
- a permeate which is a solution free of magnesium hydroxide and which is fed to a reverse osmosis unit 4, is separated off by means of the filtration stage 3.
- the concentrate retained by the membrane contains a more concentrated suspension with magnesium hydroxide, which is returned to the working container 2.
- the working tank 2 also receives pure water which, together with the filtration stage 3, serves to rinse out further salts.
- the pure water is taken from the reverse osmosis unit 4, the concentrate of which is disposed of. After this process has been run through several times, the concentrate which is retained by filtration stage 3 and which only contains highly pure magnesium hydroxide is removed.
- FIG. 2 A further exemplary embodiment of a device according to the invention for carrying out the method according to the invention, in which magnesium hydroxide is produced from a concentrate, is shown in FIG. 2.
- the device shown has a plurality of series-connected crossflow filtration stages 6 to 8 (hereinafter referred to as filter stages), each of which has a membrane filter.
- the pore size of the membrane filter is between 0.05 and 0.5 micrometers.
- the solution containing the magnesium is mixed with sodium hydroxide solution in a reaction container 5, so that the magnesium precipitates in the form of magnesium hydroxide.
- the suspension formed in this way is then fed to a first filter stage 6, with which a prefiltration is carried out.
- the permeate passing through the membrane filter of filter stage 6 in the form of water and soluble salts is discharged into a channel.
- the concentrate generated from the filter stage 6 is fed to a further filter stage 7.
- the permeate of this filter stage 7 is fed to a reverse osmosis unit 9.
- Their permeate is high-purity water and is fed to a further filter stage 8.
- the concentrate of the reverse osmosis unit 9 is discharged into a channel for disposal.
- the permeate produced by filter stage 8 only has small amounts of salts and is fed back to filter stage 7, which is connected upstream of filter stage 8, to remove further salts.
- the concentrate produced by the filter stage 8 has the high-purity magnesium hydroxide.
- FIG. 3 shows a further exemplary embodiment of a device according to the invention, which uses the method according to the invention, and a lye is added to a salt solution which contains the magnesium and is passed into a reaction container 10, as a result of which magnesium hydroxide is precipitated.
- the resulting salt solution-containing suspension is fed to a pre-filtration stage 11 downstream of the reaction container 10.
- the concentrate formed during the prefiltration is passed on to a mixer 12 downstream of the prefiltration stage 11, the function of which will be discussed in more detail below.
- the residues retained during the prefiltration are discharged into the waste water.
- the suspension passes from the mixer 12 into several filter stages 13 to 17 connected in series, the concentrate of one filter stage always being passed on to the downstream filter stage.
- the permeate leaving the individual filter stages is returned to different components of the device according to the invention, wherein it is preferably returned to upstream filter stages.
- the permeate of filter stage 15 is returned to filter stage 14 and the permeate of filter stage 17 is returned to filter stage 16.
- the permeate becomes more and more salt-free at every filter stage.
- the filter of the filter stage 16 and the permeate of a reverse osmosis unit 18, which is almost salt-free, are fed to the filter stage 17.
- the reverse osmosis unit 18 itself is supplied with either fresh water or the permeate from the filter stage 13.
- the concentrate of filter stage 17 is almost salt-free and contains almost exclusively the high-purity magnesium hydroxide.
- the method and the device according to the invention have the advantage that the permeate, which is only slightly contaminated with dissolved salts, is returned to a filter stage in an upstream filter stage for washing out the salts present there.
- this countercurrent process can be used to produce metal hydroxide in virtually any purity.
- the arrangement of filter stages shown with the large bracket in FIG. 3 can be connected in series as often as desired.
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Water Supply & Treatment (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Nanotechnology (AREA)
- Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
- Pharmaceuticals Containing Other Organic And Inorganic Compounds (AREA)
Abstract
Description
Claims
Priority Applications (7)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP03744816A EP1487743B1 (en) | 2002-03-25 | 2003-03-19 | Method and device for producing a metal hydroxide |
CA2479391A CA2479391C (en) | 2002-03-25 | 2003-03-19 | Method and apparatus for producing a metal hydroxide |
AU2003215668A AU2003215668A1 (en) | 2002-03-25 | 2003-03-19 | Method and device for producing a metal hydroxide |
US10/509,206 US7282188B2 (en) | 2002-03-25 | 2003-03-19 | Method and device for producing a metal hydroxide |
JP2003578280A JP2005527453A (en) | 2002-03-25 | 2003-03-19 | Method and apparatus for preparing metal hydroxides |
DE50308063T DE50308063D1 (en) | 2002-03-25 | 2003-03-19 | METHOD AND DEVICE FOR PRODUCING A METAL HYDROXIDE |
IL16379704A IL163797A0 (en) | 2002-03-25 | 2004-08-30 | Method and apparatus for producing a metal hydroxide |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE10213310.7 | 2002-03-25 | ||
DE10213310A DE10213310A1 (en) | 2002-03-25 | 2002-03-25 | Method and device for producing a metal hydroxide |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2003080512A1 true WO2003080512A1 (en) | 2003-10-02 |
Family
ID=27815923
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP2003/002859 WO2003080512A1 (en) | 2002-03-25 | 2003-03-19 | Method and device for producing a metal hydroxide |
Country Status (10)
Country | Link |
---|---|
US (1) | US7282188B2 (en) |
EP (1) | EP1487743B1 (en) |
JP (1) | JP2005527453A (en) |
AT (1) | ATE371628T1 (en) |
AU (1) | AU2003215668A1 (en) |
CA (1) | CA2479391C (en) |
DE (2) | DE10213310A1 (en) |
ES (1) | ES2292995T3 (en) |
IL (1) | IL163797A0 (en) |
WO (1) | WO2003080512A1 (en) |
Families Citing this family (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US7686986B2 (en) * | 2006-01-05 | 2010-03-30 | Headwaters Technology Innovation, Llc | Magnesium hydroxide nanoparticles, methods of making same and compositions incorporating same |
US9055752B2 (en) | 2008-11-06 | 2015-06-16 | Intercontinental Great Brands Llc | Shelf-stable concentrated dairy liquids and methods of forming thereof |
UA112972C2 (en) | 2010-09-08 | 2016-11-25 | Інтерконтінентал Грейт Брендс ЛЛС | LIQUID DAIRY CONCENTRATE WITH A HIGH CONTENT OF DRY SUBSTANCES |
CN103979702B (en) * | 2013-02-07 | 2016-03-09 | 上海凯鑫分离技术有限公司 | A kind of magnesium hydroxide washing water recovery process |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4865744A (en) * | 1987-07-27 | 1989-09-12 | Ciba-Geigy Corporation | Process for the continuous workup of aqueous crude dye suspensions |
US5385671A (en) * | 1992-11-03 | 1995-01-31 | Adcock Ingram Self Medication (Proprietary) Limited | Magnesium hydroxide recovery |
DE10001493A1 (en) * | 2000-01-15 | 2001-07-19 | Schneider Manfred | Magnesium hydroxide recovery, for pharmaceuticals, neutralizing agent, adsorbent or flame retardant in plastics, involves separating colloidal impurities from concentrate by cross-flow membrane filtration before precipitation |
Family Cites Families (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3819803A (en) * | 1969-06-19 | 1974-06-25 | H Tabata | Method of preparing magnesium hydroxide |
GB1317576A (en) * | 1969-10-17 | 1973-05-23 | British Periclase Co Ltd | Magnesium hydroxide production |
US4014787A (en) * | 1974-01-02 | 1977-03-29 | Systems Engineering & Manufacturing Corporation | Wastewater treatment |
US4229423A (en) * | 1979-02-09 | 1980-10-21 | Kaiser Aluminum & Chemical Corporation | Method of producing magnesium hydroxide |
SU829577A1 (en) * | 1979-08-27 | 1981-05-15 | Организация П/Я В-8413 | Method of waste water purification |
JPS59199504A (en) | 1983-04-27 | 1984-11-12 | Kurita Water Ind Ltd | Purification of ultrafine particle of metal oxide |
JPS6397289A (en) | 1986-10-13 | 1988-04-27 | Kubota Ltd | Treatment of phosphorus-containing waste water |
DE19829592C1 (en) | 1998-07-02 | 1999-12-09 | Umweltanalytisches Zentrum Gro | Mineral acids containing metals from pickling plants are processed and recovered |
DE10033478A1 (en) | 2000-07-10 | 2001-06-21 | Ralf Krupp | Sanitization of processing residues from the potash and rock salt industry comprises dissolving out soluble salts and recovering them as useful products |
-
2002
- 2002-03-25 DE DE10213310A patent/DE10213310A1/en not_active Withdrawn
-
2003
- 2003-03-19 WO PCT/EP2003/002859 patent/WO2003080512A1/en active IP Right Grant
- 2003-03-19 DE DE50308063T patent/DE50308063D1/en not_active Expired - Lifetime
- 2003-03-19 AU AU2003215668A patent/AU2003215668A1/en not_active Abandoned
- 2003-03-19 CA CA2479391A patent/CA2479391C/en not_active Expired - Fee Related
- 2003-03-19 US US10/509,206 patent/US7282188B2/en not_active Expired - Fee Related
- 2003-03-19 EP EP03744816A patent/EP1487743B1/en not_active Expired - Lifetime
- 2003-03-19 AT AT03744816T patent/ATE371628T1/en active
- 2003-03-19 ES ES03744816T patent/ES2292995T3/en not_active Expired - Lifetime
- 2003-03-19 JP JP2003578280A patent/JP2005527453A/en active Pending
-
2004
- 2004-08-30 IL IL16379704A patent/IL163797A0/en unknown
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4865744A (en) * | 1987-07-27 | 1989-09-12 | Ciba-Geigy Corporation | Process for the continuous workup of aqueous crude dye suspensions |
US5385671A (en) * | 1992-11-03 | 1995-01-31 | Adcock Ingram Self Medication (Proprietary) Limited | Magnesium hydroxide recovery |
DE10001493A1 (en) * | 2000-01-15 | 2001-07-19 | Schneider Manfred | Magnesium hydroxide recovery, for pharmaceuticals, neutralizing agent, adsorbent or flame retardant in plastics, involves separating colloidal impurities from concentrate by cross-flow membrane filtration before precipitation |
Non-Patent Citations (1)
Title |
---|
B. FRADIN, R.W. FIELD: "Crossflow microfiltration of magnesium hydroxide suspensions", SEPARATION AND PURIFICATION TECHNOLOGY, vol. 16, no. 1, 10 June 1999 (1999-06-10), pages 25 - 45, XP002247079 * |
Also Published As
Publication number | Publication date |
---|---|
ATE371628T1 (en) | 2007-09-15 |
ES2292995T3 (en) | 2008-03-16 |
CA2479391C (en) | 2012-05-22 |
AU2003215668A1 (en) | 2003-10-08 |
CA2479391A1 (en) | 2003-10-02 |
IL163797A0 (en) | 2005-12-18 |
US7282188B2 (en) | 2007-10-16 |
EP1487743B1 (en) | 2007-08-29 |
US20050127001A1 (en) | 2005-06-16 |
DE10213310A1 (en) | 2003-10-09 |
JP2005527453A (en) | 2005-09-15 |
DE50308063D1 (en) | 2007-10-11 |
EP1487743A1 (en) | 2004-12-22 |
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